Process for the removal of H2 S and adjustment of the H2 /CO ratio in gaseous streams containing hydrogen sulfide, carbon monoxide, and hydrogen

ABSTRACT

An integrated process for modifying the H 2  /CO ratio in specified gaseous streams is disclosed, the process being characterized by bulk removal of H 2  S, adjustment of H 2  /CO ratio by water gas (or carbon monoxide) shift, and removal of remaining H 2  S. CO 2  may be recovered, and the process may be operated to produce a gas comprising principally hydrogen.

BACKGROUND OF THE INVENTION

A number of gasification processes in existence or being developed,e.g., gasification of coke, residues, coal, etc., produce synthesisgases having various quantities of H₂, CO, CO₂ and H₂ S, as well asminor "impurity" components of NH₃ and HCN. In the case of synthesisgases derived from the gasification of coal, for example, the ratio ofCO to H₂ may range from 0.9 to 12:1, and the gas may contain from 0.05percent to 10 percent by volume of H₂ S. If the "syn-gas" is to be usedfor fuel purposes, the ratios mentioned are generally satisfactory, andlittle need be done except elimination of contaminants such as H₂ S andHCN.

On the other hand, if other uses for the synthesis gas are contemplated,such as hydrogen production or use as a feedstock for synthesisoperations, the ratio of H₂ to CO may become critical, and adjustment ofthe H₂ /CO ratio to the right range may require great expense.Accordingly, a process that provided a ready method of adjustment of theH₂ /CO ratio from such gases, even to the production of hydrogen alone,could have great economic importance. The invention relates to such aprocess.

SUMMARY OF THE INVENTION

Accordingly, the invention relates to a process comprising

(a) contacting a gaseous stream containing H₂, CO, and H₂ S with an H₂S-selective absorbent in an absorption zone and absorbing the bulk ofthe H₂ S in said stream, producing a partially purified gas streamcontaining a minor portion of H₂ S;

(b) contacting at least a portion of the partially purified gas streamwith a water shift catalyst in a conversion zone under conditions toreact CO and water, and converting CO and water to H₂ and CO₂, andproducing a modified gas stream having an increased ratio of H₂ to COand a minor quantity of H₂ S;

(c) passing modified gas stream to a contacting zone and contactingmodified gas stream with an aqueous reactant solution, the solutioncontaining an effective amount of an oxidizing reactant comprisingoxidizing polyvalent metal ions or a polyvalent metal chelate of an acidhaving the formula ##STR1## wherein from two to four of the groups Y areselected from acetic and propionic acid groups;

from zero to two of the groups Y are selected from 2-hydroxy ethyl,2-hydroxy propyl, and ##STR2## wherein X is selected from acetic acidand propionic acid groups; and R is ethylene, propylene or isopropyleneor alternatively cyclohexane or benzene where the two hydrogen atomsreplaced by nitrogen atoms are in the 1,2 positions; and mixturesthereof, and converting H₂ S in the modified gas stream in thecontacting zone to sulfur, and recovering a substantially sulfur-freegas stream having an increased ratio of H₂ to CO. In an additionalembodiment, the substantially sulfur-free gas stream having an increasedratio of H₂ to CO is passed to an absorption zone which contains anabsorbent selective for CO₂. Carbon dioxide is absorbed, and a gasstream having a high H₂ /CO ratio or comprising H₂ having asubstantially reduced CO₂ content is produced. The invention thusprovides an efficient method of producing a product stream containing awide range of H₂ /CO compositions, ranging to the point of virtuallypure hydrogen. Additionally, an optional embodiment provides for removalof minor quantities of COS, if present, in the streams.

DETAILED DESCRIPTION OF THE INVENTION

The source of the gaseous stream (containing H₂, CO, and H₂ S) is notcritical. Thus, the streams mentioned, i.e., streams derived from thegasification of coke, residues, coal, etc., are eminently suited to theinvention. Other streams containing the components mentioned, and inwhich it is desired to adjust the ratio of H₂ to CO and remove H₂ S, mayalso be treated according to the invention, so long as other componentstherein do not substantially adversely affect the absorbents, catalysts,etc. employed herein. In this regard, if the absorbents chosen aresensitive to HCN, removal of this contaminant before the stream istreated according to the invention is preferred. For example, the streammay be treated as described in U.S. application Ser. No. 556,255entitled Removal of HCN from Gaseous Streams, by Diaz, filed Nov. 29,1983. Streams derived from the gasification and/or partial oxidation ofgaseous or liquid hydrocarbon may be treated by the invention. The H₂ Scontent of the type of streams contemplated will vary extensively, but,in general, will range from about 0.05 percent to about 10 percent byvolume. CO content may vary considerably, and may range from about 30percent to over 80 percent by volume. H₂ content may also vary, butnormally will range from about 10 percent to about 50 percent by volume.CO₂, of course, may be present. Obviously, the concentrations of H₂ S,CO and H₂ present are not generally a limiting factor in the practice ofthe invention. In some of the most economically attractive gasificationprocesses, the CO to H₂ volume ratios may be quite high, as mentionedpreviously.

In the first step of the process, the gas stream selected is contactedor mixed with an absorbent selective for H₂ S in a manner or underconditions that will absorb the bulk of the H₂ S, preferably at least 80percent by volume. Any of the known H₂ S-selective absorbentsconventionally used (or mixtures thereof) which do not reactsubstantially with the other components of the gas stream, may beemployed. Those skilled in the art will recognize that most H₂S-selective absorbents tend to absorb CO₂, and if any of this gas ispresent, it will also be absorbed. Given these qualifications, theparticular absorbent chosen is a matter of choice. Aqueous alkali metalcarbonate and phosphate solutions, e.g., aqueous potassium and sodiumcarbonate and phosphate, carbitol (diethylene glycol monoethyl ether),and certain aqueous alkanolamines, such as alkyl diethanolamines, may beused. Suitable alkanolamines include methyldiethanolamine,triethanolamine, or one or more dipropanolamines, such asdi-n-propanolamine or diisopropanolamine. Aqueous methyldiethanolamine,triethanolamine and dipropanolamine solutions are preferred absorbents,particularly methyldiethanolamine and diisopropanolamine solutions. Thesolutions may contain very minor amounts of physical solvents, such assubstituted or unsubstituted tetra-methylene sulfones.

If diisopropanolamine is used, either high purity diisopropanolamine maybe used, or technical mixtures of dipropanolamine such as are obtainedas the by-product of diethanolamine production may be employed. Suchtechnical mixtures normally consist of more than 90% by weight ofdiisopropanolamine and 10% by weight or less of mono- andtri-propanolamines and possibly trace amounts of diethanolamine.Concentrations of aqueous alkanolamine solutions may very widely, andthose skilled in the art can adjust solution concentrations to achievesuitable absorption levels. In general, the concentration ofalkanolamine in aqueous solutions will be from 5 to 60% by weight, andpreferably between 25 to 50% by weight. If COS is present in the gas, itmay be removed in the absorbent, or may be hydrolyzed, as describedherein.

Suitable temperature and pressure relationships for different hydrogensulfide-selective absorbents are known, or can be calculated by thoseskilled in the art. In general, the temperatures employed in theabsorption zone are not critical, and a relatively wide range oftemperatures, e.g., from 0° to 100° C. may be utilized. A range of fromabout 0° to 85° C. is preferred.

Similarly, pressure conditions in the absorption zone may vary widely,depending on the pressure of the gas to be treated. For example,pressures in the absorption zone may vary from one atmosphere up to 150or even 200 atmospheres. Pressures of from 1 atmosphere to about 100atmospheres are preferred. As indicated, what is required in theabsorption zone is that the bulk of the H₂ S, preferably at least 80 or90 percent by volume, be absorbed. Given the solvents and parametersmentioned, those skilled in the art may adjust the conditions ofoperation to achieve this result. It is thus an advantage of theinvention that all of the H₂ S need not be removed at this point.

The absorption step thus produces a "purified" gas stream which has mostof the H₂ S removed, leaving a minor portion of H₂ S, e.g., less thanabout 10 percent to 20 percent by volume H₂ S in the stream. Theabsorption liquid or solvent, being "loaded" or "semi-loaded", ispreferably "regenerated" in suitable cyclic techniques, producing astream rich in H₂ S and a "lean" absorbent which can be recycled for usein the absorption steps. Suitable techniques for these procedures arewell known, and form no part of the present invention. See, for example,Canada Pat. No. 729,090, U.S. Pat. No. 3,989,811 and U.S. Pat. No.4,085,192. Thus, in the regeneration or stripping zone, temperatures maybe varied widely, the only requirement being that the temperatures besufficient to reduce the H₂ S content in the absorbent to a levelsufficient so that, when returned to the absorption zone, the absorbentwill effectively absorb H₂ S from the gas to be treated. Preferably, thetemperature should be sufficient to reduce the H₂ S content in the loadabsorbent to a level which corresponds to an equilibrium loading for anH₂ S content having less than 50 percent (preferably 10 percent) of theH₂ S content of the treated gas. Equilibrium loading conditions for H₂ Sand CO₂ at varying concentrations, temperatures and pressures fordifferent hydrogen sulfide-selective absorbents are known or can becalculated by known methods and hence need not be detailed herein. Ingeneral, temperature of from about 90° C. to 180° C., preferably from100° C. to 170° C., may be employed.

Similarly, in the regeneration or desorption zone, pressures will rangefrom about 1 atmosphere to about 3 atmospheres. As noted, thepressure-temperature relationships involved are well understood by thoseskilled in the art, and need not be detailed herein. Contact times inthe absorption zone, insofar as meaningful, will depend, inter alia, onthe velocity of the gas stream treated, the absorbent employed, and thetype of contactor employed. In a tray column, for example, contact timemight usefully be described as the total time a given volume of gas ispresent in the given absorber, recognizing the gas liquid contact maynot occur continuously in such a unit. Given these qualifications,"contact" times will normally range from 1 second to 30 seconds,preferably from 1 second to 20 seconds.

In sum, the conditions for the absorption and regeneration should be sospecified that the bulk of the H₂ S, preferably 80 to 90 percent andmost preferably at least 95 percent, by volume, of the H₂ S in the gasis absorbed. Such conditions, including choice of solvents and, e.g.,number of trays, if a tray contactor is used, will provide that verylittle CO₂ is absorbed. Any CO₂ or other gases absorbed will be releasedon regeneration, and are treated with the H₂ S, e.g., in a Claus unit.

The partially "purified" gas is now passed to a conversion zone whereinit contacts water, preferably as vapor, in the presence of a catalystfor the reaction of water and CO, and under conditions suitable for theconversion. Since one mole of water reacts with one mole of CO toproduce the hydrogen and CO₂, and since equilibrium is not easilyreached, the volume of H₂ produced varies directly with the water and COsupplied. Suitable conditions, i.e., temperatures, pressures, contacttimes, catalysts, etc., are known to those skilled in the art. Forexample, Kirk-Othmer, Encyclopedia of Chemical Technology (2nd Edition),Volume 4, pages 431 and 432 (1967), the Catalyst Handbook, Chapter 6(1970), and Catal. Rev.--Sci. Eng., Volume 21(2) pages 275-318 (1980)describe suitable conditions and catalysts for treating the purifiedstream. Appropriate catalysts include Fe/Cr for high temperature shift,and Cu/Zn for low temperature shift. The high temperature Fe-basedsupported catalysts have a higher sulfur tolerance than the Cu/Zncatalysts. However, the latter system, since it operates at lowtemperatures, can convert a higher proportion of CO and thus achieve apronounced modification of the CO/H₂ ratio. This is possible because theequilibrium of the water-shift reaction

    CO+H.sub.2 O→CO.sub.2 +H.sub.2

lies to the right at lower temperatures. As indicated, the ratio of H₂/CO is adjusted to the extent desired by controlling the volume of watersupplied to the conversion zone. Depending on the conditions applied andthe volume of H₂ S remaining in the stream, at least some COS, ifpresent, may be converted. Optionally, a COS conversion zone may beemployed after the shift zone to remove any COS present in the stream.The hydrolysis of COS is shown by the following formula:

    COS+H.sub.2 O→H.sub.2 S+CO.sub.2

Water is added, in the COS conversion zone, in the required amount. Anycatalyst demonstrating activity for this reaction may be employed.Preferred catalysts are Ni, Pd, Pt, Co, Rh or In. In general, most ofthese materials will be provided as solids deposited on a suitablesupport material, preferred amorphous support materials being thealuminas, silica aluminas, and silica. Crystalline support materialssuch as the aluminosilicates, known as molecular sieves (zeolites),synthetic or natural, may also be used. The selection of the particularcatalyst (and support, if employed) are within the skill of thoseworking in the field. Platinum on alumina is preferred.

The temperatures employed in the optional hydrolysis zone are notcritical, except in the sense that the temperatures employed will allowsubstantially complete conversion of the COS. Temperatures will rangefrom about 50° C. to 150° C. or even 200° C., although a range of fromabout 50° C. to about 150° C. is preferred. Those skilled in the art mayadjust the temperatures, as needed, to provide efficient reactiontemperatures. Contact times will range from about 0.5 second to about 10seconds, with contact times of 1 second to 3 seconds being preferred.Pressures employed in the hydrolysis zone may be atmospheric, belowatmospheric, or greater than atmospheric. If higher temperatures and ahigh temperature catalyst are employed in the shift zone, the gas streamexiting the shift reactor or the optional COS hydrolysis zone should bepassed through a heat exchange zone, the heat from the gas preferablybeing utilized to heat the gas stream entering the shift zone.

In accordance with the invention, the remainder of the H₂ S in the gasstream (and any H₂ S produced by hydrolysis) is removed by contactingthe stream with an oxidizing reactant. Suitable reactant materialsinclude oxidizing polyvalent metallic ions, (and mixtures thereof), suchas iron, vanadium, copper, manganese, and nickel, and include specifiedpolyvalent metal chelates, (and mixtures thereof), and mixtures of theions and chelates. As used herein, unless otherwise inconsistent withthe intent expressed, the term "mixtures thereof", in referring to thereactant materials indicated, includes mixtures of the polyvalent metalions, mixtures of the polyvalent metal chelates, and mixtures ofpolyvalent metal ions and polyvalent metal chelates. As noted, preferredreactants are coordination complexes in which polyvalent metals formchelates with an acid having the formula: ##STR3## wherein from two tofour of the groups Y are selected from acetic and propionic acid groups;

from zero to two of the groups Y are selected from 2-hydroxy ethyl,2-hydroxy propyl, and ##STR4## wherein X is selected from acetic acidand propionic acid groups; and R is ethylene, propylene or isopropyleneor alternatively cyclohexane or benzene where the two hydrogen atomsreplaced by nitrogen atoms are in the 1,2 position; and mixturesthereof. The oxidizing polyvalent metal should be capable of oxidizinghydrogen sulfide, while being reduced itself from a higher to a lowervalence state, and should then be oxidizable by oxygen from the lowervalence state to the higher valence state in a typical redox reaction.Iron III chelates, especially the iron III chelate ofN-(2-hydroxyethyl)ethylenediamine triacetic acid, are preferred. Otherpolyvalent metals (or chelates thereof) which can be used include lead,mercury, palladium, platinum, tungsten, nickel, chromium, cobalt,vanadium, titanium, tantalum, zirconium, molybdenum, and tin.

In accordance with the invention, a substantially sulfur-free gas streamhaving an increased H₂ /CO ratio is recovered. The conditions ofoperation of the oxidative removal of the remainder of the H₂ S from thegas stream, sulfur recovery, and regeneration of the oxidizing reactantsolution are adequately described in U.S. Pat. No. 4,409,199 (Blytas),issued Oct. 11, 1983, and U.S. Pat. No. 4,356,155, (Blytas and Diaz),issued Oct. 26, 1982, which disclosures are incorporated herein byreference.

The product produced, from this stage, will depend on the degree ofconversion in the previous shift step. The gaseous stream is treatedunder appropriate conditions with an absorbent selective for CO₂ in thepresence of H₂ or H₂ and CO. If the shift reaction has been utilized toadjust the H₂ /CO ratio to a given point, the product will be H₂ and CO,in the given ratio. On the other hand, if the CO is reacted toextinction, the gas stream product will be comprised predominantly ofhydrogen. Those skilled in the art may select appropriate CO₂ selectiveabsorbents, pressures, temperatures, etc., to separate the hydrogen/CO₂or hydrogen/CO₂ /CO mixtures. Suitable absorbents include aqueousalkanolamines, sodium or potassium carbonate solutions, tri-potassiumphosphate, or solutions of sterically-hindered amines in aqueous ororganic solvents, or in combinations of amines and potassium carbonate.Conditions for designing absorption and regeneration may be selected onthe basis of the specific case considered. Characteristics of theaqueous alkanoalmines, alkali metal carbonates, and potassiummetaphosphate are well known, as described in Gas Purification by A. L.Kohl and F. C. Riesenfeld (1960). Use of sterically-hindered amines forCO₂ absorption is described in U.S. Pat. No. 4,112,050 (1978), U.S. Pat.No. 4,112,051 (1978), and U.S. Pat. No. 4,100,257 (1978). Preferably,temperatures will range from 10° C. to 80° C., and pressures willpreferably range from 1 atmosphere to 100 atmospheres. The CO₂absorption is preferably conducted as a cyclic process in which the CO₂-"loaded" absorbent is regenerated or stripped, the "lean" absorbentbeing returned for use, and the CO₂ being recovered or vented.

Off-gases from the bulk H₂ S absorption-regeneration procedure arepreferably oxidized to produce sulfur. The liberated H₂ S is preferablytreated by that process known as the "Claus" process. In the "Claus"process, elemental sulfur is prepared by partial oxidation of the H₂ Sto sulfur dioxide, using an oxygen-containing gas (including pureoxygen), followed by the reaction of the sulfur dioxide with theremaining part of the hydrogen sulfide, in the presence of a catalyst.This process, which is used frequently at refineries, and also for theworkup of hydrogen sulfide recovered from natural gas, is carried out ina plant which typically comprises a combustion chamber followed by oneor more catalysts beds between which are arranged one or more condensersin which the reaction products are cooled and the separated liquidelemental sulfur is recovered. To some extent, the amount of elementalsulfur recovered depends on the number of catalyst beds employed in theClaus process. In principle, 98% of the total sulfur available can berecovered when three beds are used.

Since the yield of recovered elemental sulfur, relative to the hydrogensulfide introduced, is not quantitative, a certain amount of unreactedhydrogen sulfide and sulfur dioxide remains in the Claus off-gases.These gases may be incinerated in a furnace or treated in other waysknown to those skilled in the art.

In order to describe the invention with greater particularity, referenceis made to the accompanying schematic drawing. The drawing is asimplified diagram illustrating process steps of the invention and theirintegration in a process flow scheme. Incidental elements, such aspumps, valves, tanks, etc., are not shown. All values are merelyexemplary or calculated, and should not be taken as delimiting theinvention.

As shown, a gas stream containing 1.8 percent H₂ S, 5 percent CO₂, 48percent CO and 35 percent H₂ (all by volume), enters absorber orcontacter (1) via line (2). Absorber (1) is a tray contactor, althoughany suitable contacting device (such as a venturi) may be employed. Anabsorbent mixture, e.g., a mixture comprising 45 percent by volume ofwater and 55 percent by volume of sulfolane, enters contactor (1) vialine (3). For illustrative purposes, it will be assumed that the gaseousstream enters at 200 MSCF per hour, while the absorbent mixture entersat 20M gallons per hour. Pressure of the gas in line (2) is 100 PSIG,and the temperature of 45° C. The countercurrent flow of liquid and gas,as illustrated, provides for good contact and absorption of the H₂ S inthe stream. Approximately 97 percent by weight of the H₂ S in the streamis absorbed, and the partially purified gas is removed overhead via line(4).

The H₂ S-containing ("loaded") absorbent exits absorber (1) via line(5), and passes to stripping or regeneration column (6) wherein the H₂ Sis stripped from the absorbent, preferably by heat supplied as steam."Lean" absorbent is returned via line (3) for re-utilization in absorber(1) while H₂ S is removed via line (7). The H₂ S in line (7) may betreated in any suitable fashion, but is preferably sent to a Claus unit.If CO₂ has been absorbed to any extent, provision may also be made forits removal or recovery.

Upon exit from contactor (1), the gas stream, which has a substantiallyreduced H₂ S, content, passes via line (4) to reactor or contact zone(8) wherein it is contacted with water supplied via line (9) and with acatalyst containing Fe/Cr on activated alumina. The gas in line (4) ispreferably heat exchanged with the exit gas in line (10) before entryinto reactor (8). The temperature of the exit of reactor (8) is about300° C., pressure about 1000 psig, and total contact time in zone (8) is2 seconds. In this illustration, sufficient water, as vapor, is suppliedin a ratio of 0.3 mols per mol of CO in the gas stream. More or lesswater may be supplied, the determining factor being the degree ofconversion desired. If the COS in the original stream has not beenabsorbed by the absorbent in contactor (1), or if some remains in thegas stream in line (4), it may be hydrolyzed also in zone (8) to somedegree. An optional COS hydrolysis zone (11) is shown (dotted llines) inline (10), the outlet line from zone (8). Suitable catalysts andconditions for such removal are as described, supra; see theaforementioned U.S. Pat. No. 4,409,199.

In accordance with the invention, the gas stream, containing themodified gas stream, and possible COS hydrolysis products, passes vialine (10) to contactor (12) where it is contacted with an aqueousreactant solution to produce sulfur. Contactor (12) is a tray contactor,although any suitable contacting device (such as a venturi) may beemployed. An aqueous oxidizing reactant solution, e.g., a solutioncontaining 0.4 molar of the Fe(III) complex of (n-hydroxyethyl)ethylenediamine triacetic acid, enters contactor (12) via line (13). The gaseousstream enters at 225 MSCF per hour, while the reactant solution entersat 400 gallons per hour. Pressure of the gas in line (10) is 800 PSIG,and the temperature of the gas, having exchanged heat with line (4), is50° C. Reactant solution is supplied at a temperature of 40° C. Thecountercurrent flow of liquid and gas, as illustrated, provides for goodcontact and reaction of the H₂ S in the stream to sulfur. As will beunderstood by those skilled in the art, water and the Fe(III) complex orchelate of (n-hydroxyethyl)ethylene diamine triacetic acid are alsoproduced by the reaction.

Upon exit from contactor (12), the modified gas stream, which is nowsubstantially free of H₂ S, passes through line (14) to absorption zone(15), as more fully described hereinafter. Concomitantly, reactantmixture, containing some Fe(II) chelate of (n-hydroxyethyl)ethylenediamine triacetic acid and sulfur, is forwarded via line (16) toregeneration zone (17). As shown in dotted line boxes, the sulfur may beremoved prior to regeneration or after regeneration. Preferably, sulfuris removed before regeneration.

In regenerator (17), oxygen is supplied, as shown in molar excess.Preferably, the oxygen is supplied as air, in a ratio of about 2.0 orgreater per mole of Fe(II) chelate in the mixture. Temperature of themixture is preferably around 40° C., and pressure is suitably 20 to 30psig. Regeneration in this manner has the added advantage of removingsome water vapor, thus aiding in prevention of water build-up in thesystem and reducing bleed and make-up problems. It is not necessary thatall of the Fe(II) chelate be converted.

Regenerated absorbent mixture, i.e., an absorbent mixture in which atleast the bulk of the Fe(II) chelate has been converted to the Fe(III)chelate, is removed via line (13) and returned to contactor (12).

Any suitable absorbent for removing CO₂ from the H₂ /CO mixture in thestream may be employed in absorber (15). For example, aqueousdiisopropanolamine/sulfolane mixtures may be employed. Suitable CO₂absorption removal procedures and conditions are known to those skilledin the art, and form no part of the present invention. Suitably, the CO₂removal procedure is conducted with a regenerable absorbent, the desiredmodified stream being removed via line (18), and the loaded absorbentbeing removed for regeneration via line (19).

While the invention has been illustrated with particular apparatus,those skilled in the art will appreciate that, except where specified,other equivalent or analgous units may be employed. The term "zone," asemployed in the specification and claims, includes, where suitable, theuse of segmented equipment operated in series, or the division of oneunit into multiple units because of size constraints, etc. For example,an absorption column might comprise two separate columns in which thesolution from the lower portion of the first column would be introducedinto the upper portion of the second column, the gaseous material fromthe upper portion of the first column being fed into the lower portionof the second column. Parallel operation of units, is of course, wellwithin the scope of the invention.

Again, as will be understood by those skilled in the art, the solutionsor mixtures employed, e.g., the oxidizing reactant solutions, maycontain other materials or additives for given purposes. For example,U.S. Pat. No. 3,933,993 discloses the use of buffering agents, such asphosphate and carbonate buffers. Similarly, U.S. Pat. No. 4,009,251describes various additives, such as sodium oxalate, sodium formate,sodium thiosulfate, and sodium acetate, which may be beneficial.

What is claimed is:
 1. A process comprising(a) contacting a gaseousstream containing H₂, CO, and H₂ S with an H₂ S-selective absorbent inan absorption zone and absorbing the bulk of the H₂ S in said stream,producing a partially purified gas stream with water and containing aminor portion of H₂ S; (b) contacting at least a portion of thepartially purified gas stream with a water shift catalyst underconditions to react CO and water in a conversion zone, and converting COand water to H₂ and CO₂, and producing a modified gas stream havingincreased ratio of H₂ to CO and a minor portion of H₂ S; (c) passingmodified gas stream to a contacting zone and contacting modified gasstream with an aqueous reactant solution, the solution containing aneffective amount of a reactant comprising oxidizing polyvalent metalions or a polyvalent metal chelate of an acid having the formula##STR5## wherein from two to four of the groups Y are selected fromacetic and propionic acid groups;from zero to two of the groups Y areselected from 2-hydroxy ethyl, 2-hydroxy propyl, and ##STR6## wherein Xis selected from acetic acid and propionic acid groups; and R isethylene, propylene or isopropylene or alternatively cyclohexane orbenzene where the two hydrogen atoms replaced by nitrogen atoms are inthe 1,2 position; and mixtures thereof, and converting H₂ S in saidmodified gas stream to sulfur and recovering a substantially sulfur-freegas modified stream having an increased ratio of H₂ to CO.
 2. Theprocess of claim 1 wherein substantially sulfur-free modified stream ispassed to an absorption zone containing an absorbent selective for CO₂,CO₂ is absorbed, and a gas stream comprising H₂ having substantiallyreduced CO₂ content is produced.
 3. The method of claim 2 wherein CO₂ isrecovered.
 4. The process of claim 2 wherein the oxidizing reactant isthe iron III chelate of N-(2-hydroxyethyl)ethylene diamine triaceticacid.
 5. The process of claim 3 wherein the oxidizing reactant is theiron III chelate of N-(2-hydroxyethyl)ethylene diamine triacetic acid.6. The process of claim 4 wherein modified gas stream produced in step(b), prior to passing to step (c), is contacted with a COS hydrolysiscatalyst under conditions to hydrolyze COS.
 7. The process of claim 5wherein modified gas stream produced in step (b), prior to passing tostep (c), is contacted with a COS hydrolysis catalyst under conditionsto hydrolyze COS.